EP2912158B1 - Contrôle de l'humidité dans des réacteurs chimiques - Google Patents

Contrôle de l'humidité dans des réacteurs chimiques Download PDF

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Publication number
EP2912158B1
EP2912158B1 EP13786602.6A EP13786602A EP2912158B1 EP 2912158 B1 EP2912158 B1 EP 2912158B1 EP 13786602 A EP13786602 A EP 13786602A EP 2912158 B1 EP2912158 B1 EP 2912158B1
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Prior art keywords
gas
liquid
cell
reactor
chamber
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German (de)
English (en)
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EP2912158A2 (fr
Inventor
Shireen GOH
Rajeev Jagga Ram
Kevin Shao-Kwan Lee
Michelangelo Canzoneri
Horst Blum
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Sanofi SA
Massachusetts Institute of Technology
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Sanofi SA
Massachusetts Institute of Technology
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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/24—Gas permeable parts
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/26—Conditioning fluids entering or exiting the reaction vessel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/30—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration
    • C12M41/34—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration of gas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/44—Means for regulation, monitoring, measurement or control, e.g. flow regulation of volume or liquid level

Definitions

  • US5081035A discloses a system for continuous perfusion culturing of anchorage-dependent and anchorage-independent mammalian cell lines. It also discloses that in vivo capillary bed conditions are simulated by providing a bioreactor having a growth chamber wherein the cells are grown between a multitubular array comprising at least three functionally separate, inert non-degradable and structurally strong tubes or sets of tubes. A constant nutrient gradient is maintained along the entire length of the tubes by perfusing medium through the tubes at a flow rate which is sufficient to expose all areas of the chamber to fresh medium by convective forces rather than diffusion.
  • Control of humidity in chemical reactors, as well as associated systems, are generally described. Certain embodiments relate to the control of humidity within gas transport conduits.
  • the subject matter of the present invention involves, in some cases, interrelated products, alternative solutions to a particular problem, and/or a plurality of different uses of one or more systems and/or articles.
  • Control of humidity in chemical reactors and associated systems are generally described.
  • the humidity within gas transport conduits and chambers can be controlled to inhibit unwanted condensation within gas transport pathways.
  • By inhibiting condensation within gas transport pathways clogging of such pathways can be limited (or eliminated) such that transport of gas can be more easily and controllably achieved.
  • strategies for purging condensed liquid from chemical reactor systems are also described.
  • the invention described herein can be used to control evaporation and compensate for liquid loss in reactor chambers. Such control and compensation can be especially useful in small volume reactors (e.g., reactors having volumes of about 50 milliliters or less), in which the loss of even small amounts of liquids can adversely impact reactor performance.
  • the reactors described herein include a liquid phase (which can contain, for example, a liquid growth medium for biological cells such as any common cell growth medium containing essential amino acids and cofactors known to those of ordinary skill in the art) and a gas phase (e.g., comprising carbon dioxide, oxygen, and/or an inert gas).
  • the liquid phase and the gas phase can be in direct contact, while in other such embodiments, the liquid phase and the gas phase can be separated by a moveable wall, as described in more detail below.
  • the reactor system of the invention comprises a humidifier.
  • the humidifier can be connected directly or indirectly to a gas inlet of the reactor chamber.
  • the humidifier can be any vessel in which gas is transported (e.g., bubbled) through a liquid at a temperature that is equal to or higher (e.g., at least about 1°C higher, at least about 5°C higher, at least about 10°C higher, at least about 20°C higher, at least about 30°C higher, or at least about 40°C higher (and/or, in certain embodiments, up to about 50°C higher, up to about 75°C higher, or more)) than the temperature of the liquid in the reactor chamber (e.g., between about 30°C to about 40°C).
  • the humidifier can be configured to produce a humidifier gas outlet stream having a liquid vapor content that is greater than the liquid vapor content of the gas transported into the humidifier.
  • the liquid vapor content is greater than or equal to about 70% (e.g., greater than or equal to about 80%, greater than or equal to about 90%, about 100%) of the saturation point for the humidifier temperature.
  • a liquid trap can be connected to a gas outlet of the reactor chamber.
  • the liquid trap can be any vessel in which gas is transported (e.g., bubbled) through a liquid at a temperature that is equal to or lower (e.g., at least about 1°C lower, at least about 5°C lower, least about 10°C lower, or least about 20°C lower) than the temperature of the liquid in the reactor chamber.
  • the liquid trap can be configured to produce a liquid trap gas outlet stream having a liquid vapor content that is lower than the liquid vapor content of the gas transported into the liquid trap.
  • the liquid vapor content of the gas may be from about 0% to about 10% (e.g., from about 0% to about 5%).
  • liquid can be removed from gas transport lines leading to one or more inlet(s) and/or outlet(s) of the reactor chamber, for example, by flushing the lines with gas during a period of time in which there is one or more unblocked connection between an inlet and outlet of the chamber, either designed into the chamber or temporarily unblocked due to a state of the chamber.
  • the gas flow rate through the reactor chamber can be reduced (e.g., by at least about 80%, by at least about 90%, by at least about 95% (and/or, in some embodiments, by up to about 99%, or more)) by using a constriction (or other flow rate regulation device) in the gas transport conduits leading into and/or out of the chamber.
  • a constriction or other flow rate regulation device
  • the humidifier is located between the inlet constriction and the inlet of the reactor chamber.
  • the liquid trap can be located between the reactor chamber and the outlet constriction. Such positioning of the constriction can ensure that clogging of the constrictions with liquid is inhibited or eliminated.
  • FIG. 1 is a schematic illustration of a reactor system 100.
  • Reactor system 100 according to the invention comprises a reactor chamber 102.
  • Reactor system 100 according to the invention further comprises a reactor chamber gas inlet conduit 104.
  • reactor chamber gas inlet conduit 104 is configured to transport gas into reactor chamber 102 through reactor chamber gas inlet 106.
  • the reactor system 100 also comprises a flow control mechanism 108 configured to regulate the flow of gas through the reactor chamber gas inlet conduit.
  • flow control mechanism 108 corresponds to a constriction in a gas supply conduit.
  • the cross-sectional dimension of the gas supply conduit within the constriction can be, in certain embodiments, at least about 10% smaller, at least about 25% smaller, at least about 50% smaller, at least about 80% smaller, at least about 90% smaller, or at least about 95% smaller (and/or, in some embodiments, up to about 99% smaller, or smaller) than the smaller of the upstream and downstream cross-sectional diameters of the gas supply conduit, in certain embodiments.
  • flow control mechanism 108 corresponds to a pressure regulator, which generally automatically cuts off the flow of a gas at a certain pressure.
  • any suitable flow control mechanism that poses a resistance to flow may be used, such as, for example, constrictions, extensions of the gas supply conduit, impedance material in the gas supply conduit (e.g., filters), and the like.
  • flow control mechanism 108 is configured to regulate the flow of gas through the reactor chamber gas inlet conduit at a relatively low flow rate.
  • flow control mechanism 108 is configured to regulate the flow of gas through the reactor chamber gas inlet conduit at a flow rate of equal to or less than about 1 milliliter per second, equal to or less than about 100 microliters per second, or equal to or less than about 10 microliters per second (and/or in certain embodiments, as low as about 0.1 microliters per second).
  • Relatively slow transport of gas through a reactor system can be important, for example, in small-scale reactors, which might require relatively slow flows of gas to the reactor chamber.
  • reactor system 100 comprises a humidifier 110.
  • Humidifier 110 is configured to humidify the gas transported through reactor chamber gas inlet conduit 104.
  • the humidifier can comprise, for example, a fluid contained within a vessel.
  • the gas inlet conduit to the humidifier can have an outlet that is submerged in the fluid such that the gas is bubbled through the fluid within the humidifier. Subsequently, the gas can be transported out of the humidifier via a gas outlet conduit.
  • One of ordinary skill in the art would be capable of designing other schemes to achieve humidification of the gas transported through reaction chamber gas inlet conduit 104.
  • humidifier 110 is positioned between flow control mechanism 108 and reactor chamber gas inlet 106. That is to say, humidifier 110 is fluidically connected such that, after gas is transported out of flow control mechanism 108, the gas is subsequently transported through humidifier 110, and subsequently to reactor chamber 102. Positioning the humidifier in this way can reduce the degree to which liquid condenses within reactor chamber gas inlet conduit 104. In cases in which humidifier 110 is placed upstream of flow control mechanism 108, the relatively humid gas exiting the humidifier can be more prone to condense while moving relatively slowly through the narrow passageways of flow control mechanism 108. On the other hand, when humidifier 110 is placed downstream of flow control mechanism 108, the gas that is transported through flow control mechanism 108 is relatively dry, and condensation can be inhibited (or eliminated).
  • Humidifier 110 can be used, for example, to supply liquid to or maintain the level of liquid within reactor chamber 102. For example, if the liquid within reactor chamber 102 evaporates or is otherwise removed from the reaction chamber during operation, the liquid within the gas supplied by reactor chamber gas inlet conduit 104 can be transferred from the gas within reactor chamber 102 to the liquid within reaction chamber 102 (optionally, through a moveable wall such as a membrane, discussed in more detail below). If the liquid level within reactor chamber 102 is determined to be at a desired level, the amount of liquid in the gas supplied by reactor chamber gas inlet conduit 104 can be set (e.g., using humidifier 110) such that evaporation of liquid within reactor chamber 102 is inhibited or eliminated.
  • the amount of liquid in the gas supplied by reactor chamber gas inlet conduit 104 can be set (e.g., using humidifier 110) such that evaporation of liquid within reactor chamber 102 is inhibited or eliminated.
  • reactor system 100 includes a reactor chamber gas outlet conduit 112.
  • Reactor chamber gas outlet conduit 112 can be configured to transport gas out of the reactor chamber through a reactor chamber gas outlet 114.
  • gas may be transported out of the reactor chamber after a moveable wall (e.g., a flexible membrane) has been actuated, as discussed in more detail below with respect to FIGS. 2A-2C and FIG. 3 .
  • Gas might also be transported out of the reactor chamber after oxygen and/or CO 2 within the gas has been transported from the gaseous headspace to the liquid medium within the reactor chamber.
  • reactor system 100 includes a flow control mechanism 116 configured to regulate the flow of gas through reactor chamber gas outlet conduit 112. Any suitable device can be used in flow control mechanism 116, including any of those outlined above with respect to flow control mechanism 108.
  • Flow control mechanism 116 is configured to regulate the flow of gas through the reactor chamber gas inlet conduit at a relatively low flow rate of equal to or less than about 1 milliliter per second, or at any other rate mentioned above with respect to flow control mechanism 108.
  • Reactor system 100 comprises, in certain embodiments, liquid trap 118.
  • Liquid trap 118 can be configured to remove liquid vapor from the gas within reactor chamber gas outlet conduit 112.
  • Liquid trap 118 can be used, for example, to measure the amount of liquid exiting reactor chamber 102 (e.g., by measuring the change in the amount of liquid contained in the liquid trap). By determining the amount of liquid exiting reactor chamber 102, one can determine whether liquid is being lost from the reactor chamber without directly measuring the amount of liquid within the reactor chamber (which can be difficult to do, in certain circumstances).
  • liquid trap 118 is positioned between flow control mechanism 116 and reactor chamber gas outlet 114. That is to say, liquid trap 118 can be fluidically connected such that, after gas is transported out of reactor chamber 102, the gas is subsequently transported through liquid trap 118, and subsequently to flow control mechanism 116. Positioning the liquid trap in this way can reduce the degree to which liquid condenses within reactor chamber gas outlet conduit 112. In cases in which liquid trap 118 is placed downstream of flow control mechanism 116, the relatively humid gas exiting the reactor chamber can be more prone to condense while moving relatively slowly through the narrow passageways of flow control mechanism 116.
  • liquid trap 118 when liquid trap 118 is placed upstream of flow control mechanism 116, the liquid trap can be used to remove vapor from the gas before it is transported to flow control mechanism 116 (such that the gas that is transported through flow control mechanism 116 is relatively dry), and condensation can be inhibited (or eliminated).
  • an amount of liquid added to or lost from the reactor chamber can be determined using the humidifier and/or the liquid trap. This can be achieved, for example, by weighing the humidifier, the reactor chamber, and/or liquid trap. For example, one could measure the weight of the liquid in the humidifier, measure the weight of the liquid in the liquid trap, determine the liquid vapor content of the gas stream entering the humidifier, and determine the liquid vapor content of the gas stream exiting the liquid trap. After making such a determination, a mass balance could be performed to determine the amount of liquid added to or lost from the reactor chamber, optionally without weight the reactor chamber itself.
  • the amount of liquid vapor in the gas stream entering the humidifier is equal to the amount of liquid vapor in the gas stream exiting the liquid trap, then the amount of liquid added to or lost from the reactor chamber can be determined by subtracting the change in weight of the liquid trap from the change in weight of the humidifier.
  • the humidification and/or evaporation rate of the liquid in the reactor chamber can be determined by measuring the humidity of the gas passing through the inlet and outlet of the reactor chamber.
  • the uptake and/or release rate of a single or plurality of different gasses into the reactor chamber can be determined by measuring the concentration of a single or plurality of gasses in the inlet and outlet of the chamber.
  • two or more (or all) of the strategies outlined above can be used in combination with each other.
  • FIG. 1 illustrates a system in which both humidifier 110 and liquid trap 118 are present
  • reactor system 100 includes humidifier 110, but does not include liquid trap 118.
  • reactor chamber 102 comprises a gaseous headspace and a liquid medium that are in direct contact. In other embodiments, however, the gaseous headspace and liquid medium are separated by a moveable wall. Reactors employing such arrangements are described, for example, in U.S. Patent Application Serial No. 13/249,959 by Ram et al, filed September 30, 2011 , and entitled “Device and Method for Continuous Cell Culture and Other Reactions" and U.S. Patent Application Publication No. 2005/0106045 by Lee, filed November 18, 2003 , and entitled “Peristaltic Mixing and Oxygenation System,”.
  • FIGS. 2A-2C are cross-sectional schematic illustrations outlining how fluid can be transported by deflecting a moveable wall into and out of a liquid sub-chamber of a reactor chamber.
  • reactor system 200 comprises reactor chamber 202.
  • reactor chamber 202 in FIGS. 2A-2C corresponds to reactor chamber 102 in FIG. 1 .
  • Reactor chamber 202 can comprise a liquid sub-chamber 204.
  • Liquid sub-chamber 204 can be configured to contain a liquid growth medium including at least one biological cell.
  • Reactor chamber 202 can comprise, in certain embodiments, gas sub-chamber 206.
  • Gas sub-chamber 206 can be configured to contain a gaseous headspace above the liquid growth medium within liquid sub-chamber 204.
  • Reactor chamber 202 can also comprise a moveable wall 208, which can separate liquid sub-chamber 204 from gas sub-chamber 206.
  • Moveable wall 208 can comprise, for example, a flexible membrane.
  • the moveable wall is formed of a medium that is permeable to at least one gas (i.e., a gas-permeable medium).
  • moveable wall can be permeable to oxygen gas and/or carbon dioxide gas.
  • the gas within gas sub-chamber 206 can be transported to liquid sub-chamber 204, or vice versa.
  • Such transport can be useful, for example, to transport oxygen gas into a liquid medium within liquid sub-chamber 204 and/or control pH by transporting carbon dioxide into or out of liquid sub-chamber 204.
  • Reactor system 200 can comprise, in certain embodiments, a gas inlet conduit 104, which can be configured to transport gas into gas sub-chamber 206.
  • Gas inlet conduit 104 in FIGS. 2A-2C can correspond to the gas inlet conduit 104 illustrated in FIG. 1 , in certain embodiments.
  • the gas that is transported into gas sub-chamber 206 can originate from, for example, gas source 216. Any suitable source of gas can be used as gas source 216, such as gas cylinders. In certain embodiments, gas source 216 is a source of oxygen and/or carbon dioxide.
  • reactor system 200 comprises gas outlet conduit 112 configured to transport gas out of gas sub-chamber 206.
  • Gas outlet conduit 112 in FIGS. 2A-2C can correspond to the gas outlet conduit 112 illustrated in FIG. 1 , in certain embodiments.
  • reactor system 200 comprises gas bypass conduit 210 connecting gas inlet conduit 104 to gas outlet conduit 112.
  • Gas bypass conduit 210 can be configured such that it is external to reactor chamber 202, in certain embodiments.
  • the set of embodiments illustrated in FIG. 1 can also include a gas bypass conduit, illustrated as conduit 210.
  • Reactor system 200 can also comprise, in certain embodiments, a liquid inlet conduit 212 and a liquid outlet conduit 214.
  • moveable wall 208 can be actuated such that the volumes of liquid sub-chamber 204 and gas sub-chamber 206 are modified.
  • certain embodiments involve transporting a gas from gas source 216 through gas inlet conduit 104 to gas sub-chamber 206 to deform moveable wall 208.
  • Deformation of moveable wall 208 can be achieved, for example, by configuring reactor 200 such that gas sub-chamber 206 is pressurized when gas is transported into gas sub-chamber 206.
  • Such pressurization can be achieved, for example, by restricting the flow of gas out of gas outlet conduit 112 (e.g., using valves or other appropriate flow restriction mechanisms) while gas is being supplied to gas sub-chamber 206.
  • deforming moveable wall 208 can result in liquid being at least partially removed from liquid sub-chamber 204.
  • moveable wall 208 has been deformed such that substantially all of the liquid within liquid sub-chamber 204 has been removed from reactor chamber 202.
  • Such operation can be used to transport the liquid within liquid sub-chamber 204 to other liquid sub-chambers in other reactors, as illustrated, for example, in FIG. 3 , described in more detail below.
  • the supply of the gas to gas sub-chamber 206 can be reduced such that moveable wall 208 returns toward its original position (e.g., the position illustrated in FIG. 2A ).
  • moveable wall 208 will be deflected such that at least a portion of the gas within gas sub-chamber 206 is removed from the gas sub-chamber.
  • gas might be removed, for example, if liquid enters liquid sub-chamber 204 from liquid inlet 212, for example, from another upstream reactor, as described in more detail below.
  • Certain embodiments include the step of supplying gas from gas source 216 to gas sub-chamber 206 at least a second time (and, in certain embodiments, at least 10 times, at least 100 times, or more) to deform moveable wall 208 such that liquid is at least partially removed from liquid sub-chamber 204.
  • moveable wall 208 can act as part of a pumping mechanism, transporting liquid into and out of liquid sub-chamber 204. Such operation is described in detail in U.S. Patent Application Serial No.
  • the multiple steps of supplying gas from gas source 216 to gas sub-chamber 206 can be performed relatively rapidly (e.g., in certain embodiments, at frequencies of between about 0.1 Hertz and about 1000 Hertz, between about 0.5 Hertz and about 10 Hertz, or between about 1 Hertz and about 3 Hertz).
  • gas can be transported from the gas source through gas bypass conduit 210.
  • Transporting gas through gas bypass conduit 210 can be performed to remove liquid from gas inlet conduit 104 without transporting the liquid to gas sub-chamber 206.
  • a first valve between gas bypass conduit 210 and gas inlet 106 can be closed and a second valve between gas bypass conduit 210 and gas outlet 114 can be closed (and any valves within gas bypass conduit 210 can be opened) such that, when gas is transported through gas inlet conduit 104, the gas is re-routed through gas bypass conduit 210, and subsequently out gas outlet conduit 112.
  • gas can be transported through the bypass conduit 210 (e.g., as described above) in between steps of transporting gas into gas sub-chamber 206 (e.g., to actuate the moveable wall, as described below), which steps can be, as described above, performed relatively rapidly.
  • FIG. 3 is a bottom view, cross-sectional schematic diagram illustrating the liquid flow paths that can be used to establish mixing between multiple reactor chambers 102A-C connected in series, as described in U.S. Patent Application Serial No. 13/249,959 by Ram et al, filed September 30, 2011 , and entitled "Device and Method for Continuous Cell Culture and Other Reactions.”
  • reactor system 300 includes a first fluidic pathway indicated by arrows 310.
  • the first fluidic pathway can include a first reactor chamber 102A, a second reactor chamber 102B, and a third reactor chamber 102C.
  • Reactor system 300 also includes conduits 321, 322, and 323, which can correspond to liquid inlet and/or liquid outlet conduits for reactor chambers 102A-C. For example, in FIG.
  • conduit 321 is a liquid inlet conduit for reactor chamber 102B and a liquid outlet conduit for reactor chamber 102A
  • conduit 322 is a liquid inlet conduit for reactor chamber 102C and a liquid outlet conduit for reactor chamber 102B
  • conduit 323 is a liquid inlet conduit for reactor chamber 102A and a liquid outlet conduit for reactor chamber 102C.
  • the flow of liquid can also be reversed such that conduits 321, 322, and 323 assume opposite roles with respect to each of reactor chambers 102A-C.
  • Reactor system 300 can also include a liquid input conduit 350 and a liquid output conduit 351, which can be used to transport liquid into and out of the liquid sub-chambers within reactor chambers 102A, 102B, and 102C.
  • Valve 352 may be located in liquid input conduit 350, and valve 353 may be located in liquid output conduit 351 to inhibit or prevent to the flow of liquid out of the mixing system during operation.
  • the moveable walls of reactor chambers 102A-C can be actuated to transport liquid along fluidic pathway 310 (and/or along a fluidic pathway in a direction opposite pathway 310). This can be achieved, for example, by sequentially actuating the moveable walls within reactor chambers 102A-C such that liquid is transported in a controlled direction.
  • each of reactor chambers 102A-C can be configured such that they are each able to assume a closed position wherein moveable wall 208 is strained such that the volume of the liquid sub-chamber is reduced, for example, as illustrated in FIG. 2B .
  • Peristaltic mixing can be achieved, for example, by actuating reactor chambers 102A-C such that their operating states alternate between open ( FIGS.2A or FIG. 2C ) and closed ( FIG. 2B ) configurations.
  • three patterns may be employed to achieve peristaltic pumping: a first pattern in which the liquid sub-chamber of reactor chamber 102A is closed and the liquid sub-chambers within reactor chambers 102B and 102C are open; a second pattern in which the liquid sub-chamber of reactor chamber 102B is closed and the liquid sub-chambers within reactor chambers 102A and 102C are open; and a third pattern in which the liquid sub-chamber of reactor chamber 102C is closed and the liquid sub-chambers within reactor chambers 102A and 102B are open.
  • liquid can be transported among reactor chambers 102A-C in a clockwise direction (as illustrated in FIGS. 2A-2B ).
  • liquid can be transported in the counter-clockwise direction as well.
  • the reactor systems described herein can be used as bioreactors.
  • the reactor systems can be configured to culture biological cells.
  • a liquid growth medium containing at least one cell is contained within the reactor chamber to achieve cell growth.
  • the liquid growth medium can contain any type of biological cell or cell type.
  • the cell may be a bacterium (e.g., E. coli) or other single-cell organism, a plant cell, or an animal cell.
  • the cell may be a eukaryotic cell. If the cell is a single-cell organism, then the cell may be, for example, a protozoan, a trypanosome, an amoeba, a yeast cell, algae, etc.
  • the cell may be, for example, an invertebrate cell (e.g., a cell from a fruit fly), a fish cell (e.g., a zebrafish cell), an amphibian cell (e.g., a frog cell), a reptile cell, a bird cell, or a mammalian cell such as a primate cell, a bovine cell, a horse cell, a porcine cell, a goat cell, a dog cell, a cat cell, or a cell from a rodent such as a rat or a mouse.
  • the cell can be a human cell.
  • the cell may be a hamster cell, such as a Chinese hamster ovary (CHO) cell.
  • the cell may be from any part of the organism.
  • the cell may be a cardiac cell, a fibroblast, a keratinocyte, a heptaocyte, a chondracyte, a neural cell, a osteocyte, a muscle cell, a blood cell, an endothelial cell, an immune cell (e.g., a T-cell, a B-cell, a macrophage, a neutrophil, a basophil, a mast cell, an eosinophil), a stem cell, etc.
  • the cell may be a genetically engineered cell.
  • the reactor chamber can, in some embodiments, be configured to contain (and/or, can contain during operation of the reactor) a volume of liquid medium equal to or less than about 50 milliliters, equal to or less than about 10 milliliters, or equal to or less than about 2 milliliters (and/or, in certain embodiments, equal to or greater than 10 microliters, equal to or greater than 100 microliters, or equal to or greater than 1 milliliter).
  • the reactor chamber has an aspect ratio of less than about 10 (or less than about 8, such as between about 5 and about 8), as measured by dividing the largest cross sectional dimension of the chamber by the smallest cross-sectional dimension of the chamber.
  • This example describes the design and operation of a reactor system integrating inventive humidity control methods.
  • evaporation compensation by injecting sterile water can be used for long term cultures. This can be achieved, for example, by refilling the reactor chamber with sterile water (e.g., every few hours).
  • Such methods can work well for fixed working volume cultures, such as chemostat cultures.
  • the volume of the culture medium might be irregular throughout the culture due to offline sampling and feeding. In such cultures, it can be very challenging (or impossible) to implement closed loop correction for evaporation at all times, and generally, the evaporation rate would need to be determined beforehand through a separate experiment.
  • Other methods of evaporation compensation are known, but most require the volume of the micro-bioreactor to be kept constant throughout the culture.
  • the slow mixing rate for culturing the CHO cells can cause water to condense within the air lines, a problem that is not seen as much when air flow is faster, as might be observed in many bacteria cultures. Condensation can be especially problematic when remote humidifiers are used as shown in FIG. 4A due to the long path that is unheated between the humidifier and the micro-bioreactor. The problem can be further exacerbated when there are air resistance lines, such as air resistance lines configured to reduce shear stress in the growth chamber. The viscosity of water is two orders of magnitude higher than air and in the narrow resistance channels. Accordingly, when water plugs the air channels, the flow rate of water is so slow that the membrane does not deflect at all within the duration of the mixer activation.
  • a new humidification strategy is illustrated in the schematic illustration of FIG. 4B .
  • the new strategy employs a local humidifier (e.g., set at 45 °C) and a water trap (e.g., set at 25 °C).
  • a local humidifier e.g., set at 45 °C
  • a water trap e.g., set at 25 °C.
  • This configuration prevents the humidified air from ever coming into contact with the solenoid valves, which will ensure a longer lifetime of the valves.
  • the resistance lines are placed before the humidifier and after the water trap; accordingly, only dry air passes through the resistance lines to prevent any potential clogging of the resistance lines with condensed water.
  • the additional water trap can act as a hydraulic equivalent of a capacitor on the mixer resistance, allowing the membrane deflection time to be increased since a high capacitance can increase the time constant of the deflection. This means that the resistance channels can be made wider and if there is any residual water in the channel, the droplet will be able to move faster in a wider channel.
  • the mixer now has separate input and output gas lines to enable flushing of the lines in case any part of the air lines get clogged. This flushing process will be performed periodically through the experiments and runs through the bypass conduit on top of the mixers, as shown in FIG. 4B .
  • the evaporation rate for the RECA Micro-bioreactor should be characterized prior to performing the cell culture experiment.
  • the increase in concentration of green food dye injected into the growth chamber is used as a parameter to calculate the evaporation rate.
  • an intensive variable measurement will be more accurate than an extensive variable (e.g. volume or mass) measurement since the error is larger for an extensive variable and the characterization will be heavily dependent on the experimental procedure.
  • the RECA Micro-bioreactor has an optical density (OD) sensor integrated, using the OD sensor to measure the light scattered/absorbed from the green dye is an accurate way to obtain the evaporation rate, ⁇ .
  • C t C o 1 ⁇ ⁇ / V t
  • C(t) is the concentration of the food dye as a function of time
  • C o is the initial concentration of food dye
  • V is the volume of liquid in the growth chamber (2mL). Since the evaporation rate is not expected to be very high, typically of the order of 1-10 ⁇ L / hr , the experiment is performed overnight (7-8 hours) to obtain a higher accuracy. The measured evaporation rate with a local 45°C humidifier attached is 4.7 ⁇ L/hr. If this evaporation is uncompensated, 75% of the volume of the micro-bioreactor will have evaporated by the end of a 14 day experiment. This could significantly increase the osmolarity of the medium and inhibit growth.
  • the strategies outlined above can be used with a new reactor design, referred to in this example as the Resistive Evaporation Compensated Actuator (RECA) micro-bioreactor, which is illustrated in FIG. 5 .
  • the reactor includes 5 reservoirs for injections, including one containing sterile water for evaporation compensation.
  • the other four reservoirs can be used for Sodium Bicarbonate (NaHCO 3 ) base injections, feed, and other necessary supplements.
  • Injection can be performed by a peristaltic pump actuated through the PDMS membrane sequentially pushing a plug of fluid into the growth chamber.
  • the growth chamber has a volume of 2 milliliters.
  • Uniform mixing can be obtained by pushing fluids through small channels connecting the three growth chambers, each having a volume of 1 milliliter.
  • a 10 microliter reservoir for sampling located after the growth chamber. The sampling can be performed via peristaltic pumping of 10 microliter plugs.
  • the sample reservoir is also connected via a channel to the sterile water line and a clean air line. Air can be injected through the sample reservoir to eject any remaining sample into the sampling container (e.g. an Eppendorf tube), and water can be injected after that to clean the sample reservoir and remove any cell culture or cells remaining. Clean air can then be sent through the reservoir to dry the chambers so that there would no water left to dilute the next sample. This process can be repeated after each sampling step.
  • the connections from the RECA micro-bioreactor to the gas manifold are shown in FIG. 6 .
  • All reservoir input valves can share the same gas line since it is unnecessary to individually control each input valve.
  • the reservoir pressure can be set to be 1.5 psi (1.03 ⁇ 10 5 Pa), which is lower than that of the mixing pressure of 3 psi (2.06 ⁇ 10 5 Pa).
  • the reservoir pressure can be used to ensure that the input to the peristaltic pumps sees the same pressure and is unaffected by external hydrostatic pressure to ensure consistent pumping volume.
  • the output of the reservoir i.e. the injection valves, can be individually controlled by separate gas lines because these are the valves that determine which feed lines are being injected into the growth chamber. Next are the gas lines that control the peristaltic pumps.
  • the mixers can have a separate input and output line in order to allow flushing of water condensation on the mixer lines, since the air coming into the mixer can be humidified to reduce evaporation of the growth culture.
  • the growth chambers of the micro-bioreactor have large surface to volume ratios and hence, the evaporation rates are generally larger than that for larger bioreactors.
  • all three mixer gas lines can be designed to have the same resistance, to ensure an even mixing rate in the 3 growth chambers.
  • the mixer gas lines can be made wider than the rest of the lines because the air is humidified, and any condensation might clog the lines if the resistance is too high.
  • the last air lines control the valves to the sampling port.
  • the sampling port consists of a 10 microliter sample reservoir and valves to control sampling and automated cleaning of the sampling port.
  • the holes in the top left corner can be sealed with a polycarbonate cover and taped with double sided tape.
  • the air lines can be connected through a group of 20 barbs located on the left bottom corner of the chip to the gas manifold.
  • a gas manifold can be used to connect the solenoid valves to the air lines of the micro-bioreactor.
  • the design of the gas manifold is shown in FIG. 7 .
  • the manifold in this example has 3 layers.
  • the barb connectors to the micro-bioreactor are situated in the center of the top layer of the manifold.
  • the middle layer routes the output of the solenoid valves to the barb connectors that connects the manifold to the micro-bioreactor.
  • the bottom layer routes the main air lines to the inputs of the solenoid valves.
  • Tables 1A-C lists all the valves with their numbers as shown in FIG. 7 and the gas connections for easier referencing.
  • Table 1A for Valves 1-8 Valve Name NO NC 1 Gas Mix 1 Gas Mix 2 (3 Psi) Gas Mix 2 (3 Psi) 2 Reservoir Input Valve On (15 Psi) Valve Off (Atm) 3 Injection 1 Valve On (15 Psi) Valve Off (Atm) 4 Injection 2 Valve On (15 Psi) Valve Off (Atm) 5 Injection 3 Valve On (15 Psi) Valve Off (Atm) 6 Injection 4 Valve On (15 Psi) Valve Off (Atm) 7 Injection 5 (water) Valve On (15 Psi) Valve Off (Atm) 8 Pump 1 Valve On (15 Psi) Valve Off (Atm) Table 1B for Valves 9-16 Valve Name NO NC 9 Gas Mix 2 Nitrogen (3 Psi) Oxygen (3 Psi) 10 Pump 2 Valve Off (Atm) Valve On (15 Psi) 11 Pump 3 Valve On (15 Psi) Valve Off (Atm) 12 Sample Reservoir Valve
  • nitrogen (N 2 ) gas can be achieved by changing the duty cycle of Gas Mix 3 solenoid valve.
  • Oxygen (O 2 ) gas concentration can be controlled via Gas Mix 2 via the same strategy. Then the two outputs can be mixed together in a 50-50 duty cycle using Gas Mix 1.
  • Gas Mix 4 is available for use if any extra valving is needed.
  • a laptop can be used to control a Field-programmable Gate Array (FPGA) board, which can control the solenoid boards, the heater board, and photo-detector board.
  • FPGA Field-programmable Gate Array
  • Air lines can be connected to a pressure regulator before being connected to the gas manifold. From the gas manifold, the valve lines can be connected directly to the micro-bioreactor.
  • the mixer in lines are connected first through an air resistance line, followed by a 45 °C local humidifier before reaching the micro-bioreactor.
  • the mixer out lines from the micro-bioreactor are connected to the water trap, then to the air resistance lines and then only to the gas manifold.
  • a reference to "A and/or B,” when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A without B (optionally including elements other than B); in another embodiment, to B without A (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc.
  • the phrase "at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements.
  • This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase "at least one" refers, whether related or unrelated to those elements specifically identified.
  • At least one of A and B can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc.

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Claims (8)

  1. Système de réacteur, comprenant :
    une chambre de réacteur ;
    un conduit d'entrée de gaz de chambre de réacteur configuré pour transporter du gaz dans la chambre de réacteur à travers une entrée de gaz de chambre de réacteur ;
    un mécanisme de contrôle du débit configuré pour réguler le débit de gaz à travers le conduit d'entrée de gaz de la chambre du réacteur à un taux égal ou inférieur à environ 1 millilitre par seconde ; et
    un humidificateur configuré pour humidifier le gaz transporté à travers le conduit d'entrée de gaz de la chambre du réacteur, l'humidificateur étant positionné entre le mécanisme de contrôle du débit et l'entrée de gaz de la chambre du réacteur.
  2. Système de réacteur selon la revendication 1, dans lequel la chambre de réacteur contient un liquide et au moins une cellule biologique.
  3. Système de réacteur selon la revendication 2, dans laquelle la cellule biologique est :
    i) une cellule eucaryote ; et/ou
    ii) une cellule de mammifère, éventuellement dans lequel la cellule de mammifère est choisie dans le groupe constitué par des cellules de primate, des cellules de bovins, des cellules de cheval, des cellules de porc, des cellules de chèvre, des cellules de chien, des cellules de chat, des cellules de rongeur, des cellules humaines et des cellules de hamster, de préférence la cellule de mammifère est une cellule d'ovaire de hamster chinois (CHO) ; et/ou
    iii) une cellule cardiaque, un fibroblaste, un kératinocyte, un hépatocyte, un chondrocyte, une cellule neurale, un ostéocyte, une cellule musculaire, une cellule sanguine, une cellule endothéliale, une cellule immunitaire ou une cellule souche.
  4. Système de réacteur selon l'une quelconque des revendications 1 à 3, dans lequel la chambre de réacteur présente un volume inférieur ou égal à 50 millilitres et/ou dans lequel le gaz comprend du dioxyde de carbone et/ou de l'oxygène.
  5. Système de réacteur selon l'une quelconque des revendications 1 à 4, dans lequel l'humidificateur comprend un récipient contenant un premier liquide présentant une température supérieure d'au moins environ 1 °C à la température de la phase liquide.
  6. Système de réacteur selon l'une quelconque des revendications 1 à 5, dans lequel le mécanisme de contrôle de débit comprend un conduit d'alimentation en gaz comprenant un étranglement, éventuellement dans lequel une dimension de section transversale du conduit d'alimentation en gaz à l'intérieur de l'étranglement est au moins 10 % inférieure aux dimensions de section transversale du conduit d'alimentation en gaz à des emplacements en amont et en aval de l'étranglement.
  7. Système de réacteur selon l'une quelconque des revendications 1 à 6, dans lequel le mécanisme de contrôle du débit comprend un régulateur de pression.
  8. Système de réacteur selon l'une quelconque des revendications 1 à 7, dans lequel la chambre de réacteur est configurée pour contenir un volume du milieu liquide qui est égal ou inférieur à 50 millilitres et égal ou supérieur à 10 microlitres.
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SG11201502926TA (en) 2015-05-28
CN104812887B (zh) 2017-11-03
HK1212726A1 (zh) 2016-06-17
US10472602B2 (en) 2019-11-12
CA2887987C (fr) 2023-02-21
US20140120609A1 (en) 2014-05-01
WO2014066781A2 (fr) 2014-05-01
AU2017279710B2 (en) 2019-09-19
EP4036208A1 (fr) 2022-08-03
CA2887987A1 (fr) 2014-05-01
CN104812887A (zh) 2015-07-29
US20200040298A1 (en) 2020-02-06
CN107557270A (zh) 2018-01-09
SG10201704655SA (en) 2017-07-28
US11725176B2 (en) 2023-08-15
MX2020004386A (es) 2020-08-20
AU2019283934A1 (en) 2020-01-23
MX2015005285A (es) 2015-11-16
CN107557270B (zh) 2021-12-07
CA3182497A1 (fr) 2014-05-01
AU2017279710A1 (en) 2018-01-25
EP2912158A2 (fr) 2015-09-02
WO2014066781A3 (fr) 2014-07-17
AU2013334175A1 (en) 2015-04-30
IN2015DN03033A (fr) 2015-09-18
US11459538B2 (en) 2022-10-04
AU2013334175B2 (en) 2017-09-28

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